CN112041264B - Method of movable pressure swing adsorption oxygen production device - Google Patents
Method of movable pressure swing adsorption oxygen production device Download PDFInfo
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- CN112041264B CN112041264B CN202080001896.9A CN202080001896A CN112041264B CN 112041264 B CN112041264 B CN 112041264B CN 202080001896 A CN202080001896 A CN 202080001896A CN 112041264 B CN112041264 B CN 112041264B
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 662
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 221
- 239000001301 oxygen Substances 0.000 title claims abstract description 221
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 221
- 238000000034 method Methods 0.000 title claims abstract description 66
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 146
- 239000007789 gas Substances 0.000 claims abstract description 115
- 239000003463 adsorbent Substances 0.000 claims abstract description 97
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 73
- 239000002994 raw material Substances 0.000 claims abstract description 27
- 238000006073 displacement reaction Methods 0.000 claims abstract description 12
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 74
- 229910052786 argon Inorganic materials 0.000 claims description 37
- 239000002808 molecular sieve Substances 0.000 claims description 24
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 24
- 238000001035 drying Methods 0.000 claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 239000002274 desiccant Substances 0.000 claims description 8
- 229910052744 lithium Inorganic materials 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- 238000010926 purge Methods 0.000 claims description 8
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 4
- 238000003795 desorption Methods 0.000 claims description 2
- 230000036284 oxygen consumption Effects 0.000 abstract description 6
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 18
- 238000005086 pumping Methods 0.000 description 18
- 229920006395 saturated elastomer Polymers 0.000 description 9
- 238000010586 diagram Methods 0.000 description 8
- 230000000630 rising effect Effects 0.000 description 5
- 238000000605 extraction Methods 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 238000013459 approach Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 230000000754 repressing effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
- C01B13/0229—Purification or separation processes
- C01B13/0248—Physical processing only
- C01B13/0259—Physical processing only by adsorption on solids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/12—Oxygen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/40062—Four
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- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention provides a method of a movable pressure swing adsorption oxygen production device, which comprises a first pressure swing adsorption section and a second pressure swing adsorption section which are operated in series, wherein most of nitrogen in dry raw material air is adsorbed by a nitrogen balance selective adsorbent bed layer of the first pressure swing adsorption section, oxygen-enriched mixed gas flows into a speed selective adsorbent bed layer of the second pressure swing adsorption section, so that oxygen is adsorbed by the speed selective adsorbent bed layer, and the second pressure swing adsorption section analyzes high-concentration oxygen; the adsorption tower of the first pressure swing adsorption section sequentially undergoes at least four steps of adsorption A, pressure equalizing and ED reducing, reverse discharge BD or vacuumizing VC and pressure equalizing and ER lifting in a cycle period; the adsorption tower of the second pressure swing adsorption section is at least sequentially subjected to the steps of adsorption A, product oxygen displacement P, vacuumizing VC and serial adsorption A1 in a cycle period. The pressure swing adsorption device adopting the method has the advantages of small volume, light weight, convenient use and low pressure, greatly reduces the oxygen consumption cost and obviously improves the oxygen consumption safety.
Description
Technical Field
The invention relates to the field of pressure swing adsorption technology oxygen production, in particular to a method of a movable pressure swing adsorption oxygen production device.
Background
At present, pure oxygen used in the gas cutting process is prepared by adopting a deep cooling device, the pure oxygen is compressed to more than 12.5MPa by using a compressor and then is filled into a specially-made 40-liter steel cylinder, and then the steel cylinder is transported to each user, and the user using pressure is lower than 0.95MPa, so that a large amount of manpower and material resources are consumed, the oxygen consumption cost is high, and the safety is poor.
Disclosure of Invention
Aiming at the problems, the invention aims to provide a method of a movable pressure swing adsorption oxygen production device which has small volume, light weight, convenient use and low pressure, is started and stopped at any time, greatly reduces the oxygen consumption cost and greatly improves the oxygen consumption safety. The invention aims at realizing the following technical scheme:
a method for preparing oxygen production device by mobile pressure swing adsorption includes such steps as serially connecting two sections of pressure swing adsorption, loading raw air without gaseous water to nitrogen balance selective adsorbent bed from bottom of adsorption tower, adsorbing most of nitrogen in raw air by nitrogen balance selective adsorbent bed, loading most of oxygen and argon to speed selective adsorbent bed from bottom of adsorption tower, adsorbing oxygen-enriched gas by speed selective adsorbent bed, and eluting nitrogen and argon and small amount of oxygen from outlet of adsorption tower. The adsorption tower of the first pressure swing adsorption section sequentially undergoes four pressure swing adsorption process steps of adsorption A, pressure equalizing and reducing ED, reverse discharge BD or vacuumizing VC and pressure equalizing and lifting ER in a cycle period; the adsorption tower of the second pressure swing adsorption section sequentially undergoes the pressure swing adsorption process steps of adsorption A, product oxygen displacement P, vacuumizing VC and serial adsorption A1 in a cycle period.
Further, the adsorption tower of the second pressure swing adsorption section is added with a serial replacement P1 step after the adsorption A step, and the replacement gas of the serial replacement step is from the mixed gas discharged from the outlet of the other adsorption tower in the product oxygen replacement P step.
Further, the adsorption tower of the first pressure swing adsorption section is added with a final step of boosting FR after the step of equalizing pressure and boosting ER, and the boosted gas of the step is from the oxygen-enriched mixed gas at the outlet of the adsorption tower adsorption A step of the first section.
In view of the fact that the feed air may contain gaseous water, to ensure the adsorption effect of the nitrogen balance selective adsorbent bed of the first pressure swing adsorption stage, the feed air needs to be dried, for which two solutions are provided by the present invention:
scheme 1: the bottom of the first section adsorption tower is filled with a drying agent, the upper part of the first section adsorption tower is filled with a nitrogen balance selective adsorbent bed, most of gaseous water in raw material air is adsorbed by the drying agent bed when passing through the bottom of the first section adsorption tower, most of nitrogen is adsorbed by the nitrogen balance selective adsorbent bed, most of oxygen and argon flow out from an outlet of the adsorption tower and enter the speed selective adsorbent bed from the bottom of the adsorption tower of the second pressure swing adsorption section, oxygen-enriched air is adsorbed by the speed selective adsorbent bed, nitrogen and argon flow out from an outlet of the adsorption tower, and a small amount of oxygen flows out from the outlet of the adsorption tower, and the analyzed mixed gas is high-concentration oxygen.
Scheme 2: the pressure swing adsorption drying section is additionally arranged in front of the first pressure swing adsorption section and is used for removing gaseous water in the air, so that the requirement of the adsorption tower entering the first pressure swing adsorption section on moisture is met. The pressure swing adsorption drying section sequentially goes through two pressure swing adsorption process steps of adsorption A and purging P in a cycle period, and the gas in the purging P step is sourced from the vent gas of the adsorption A step outlet of the adsorption tower of the first pressure swing adsorption section and the desorption vent gas of the adsorption tower of the second pressure swing adsorption section. The drying section is filled with active alumina as a drying agent; the adsorption tower of the first pressure swing adsorption section is internally filled with a 5A type molecular sieve or an X type lithium molecular sieve as a nitrogen balance selective adsorbent; the adsorption tower of the second pressure swing adsorption section is filled with carbon molecular sieve as a speed selective adsorbent.
Further, the pressure of the adsorption tower adsorption A step of the first pressure swing adsorption section and the second pressure swing adsorption section is 0.005-0.2MPa (gauge pressure).
Further, the concentration of oxygen in the outlet gas at the end of the adsorption step A of the adsorption tower of the first pressure swing adsorption section is 70-80% (V).
Further, the adsorption tower of the first pressure swing adsorption section is filled with a 5A type molecular sieve or an X type lithium molecular sieve; the adsorption tower of the second pressure swing adsorption section is filled with carbon molecular sieves.
The movable pressure swing adsorption pure oxygen production device provided by the method of the invention greatly reduces the oxygen consumption cost and greatly improves the safety, and has the advantages of small volume, light weight, convenient use after starting and stopping, and the highest pressure is only 1.2MPa.
Drawings
FIG. 1 is a timing chart showing the operation steps of the adsorption tower and the switching of the programmable valve in each section of embodiment 1 of the present invention.
Fig. 2 is a process flow diagram of example 1 of the present invention.
FIG. 3 is a timing chart showing the operation steps of the adsorption tower and the switching of the programmable valve according to the embodiment 2 of the present invention.
Fig. 4 is a process flow diagram of embodiment 2 of the present invention.
FIG. 5 is a timing chart showing the operation steps of the adsorption tower and the switching of the programmable valve in each section of embodiment 3 of the present invention.
Fig. 6 is a process flow diagram of example 3 of the present invention.
FIG. 7 is a timing chart showing the operation steps of the adsorption tower and the switching of the programmable valve according to the embodiment 4 of the present invention.
Fig. 8 is a process flow diagram of example 4 of the present invention.
Best mode for carrying out the invention
The following description of the preferred embodiments of the present invention is given for the convenience of understanding the technical solution of the present invention only, and is not to be taken as limiting the scope of the claims of the present invention.
Example 1:
FIG. 1 is a timing chart showing the operation steps of the adsorption tower and the switching of the programmable valve in each section of embodiment 1 of the present invention.
Fig. 2 is a process flow diagram of example 1 of the present invention.
The raw material air composition of this example is as follows:
| the components | O 2 | N 2 | Ar | CO 2 | Others | ∑ |
| Concentration (%) (V) | 20.93 | 78.03 | 0.932 | 0.03 | 0.078 | 100 |
Temperature: the temperature is less than or equal to 40 DEG C
Pressure: 0.05MPa (G)
As shown in fig. 2, a first pressure swing adsorption section is formed by a vacuum pump P0101, a vacuum buffer tank V0101, a program-controlled valve, a PLC control system, instruments and meters, process pipeline pipes, adsorption towers T0101A and T0101B, and the adsorbent filled in the adsorption towers is a 5A molecular sieve or a lithium molecular sieve, so that a single-tower adsorption, pressure equalizing and vacuumizing procedure is operated; pure oxygen vacuum pump P0201, pure oxygen compressor C0201, oxygen boosting buffer tank V0201, compressor buffer tank V0202, product pure oxygen buffer tank V0203, program control valve, PLC control system, instrument and meter, process pipeline pipe fitting, adsorption tower T0201A, T0201B, T0201C and T0201D constitute the second pressure swing adsorption section, and the adsorbent that packs in the adsorption tower is carbon molecular sieve, operation single tower adsorption, displacement and evacuation procedure. In this embodiment, the two sections of pressure swing adsorption are operated in series, the first pressure swing adsorption section adsorbs nitrogen in air, and the second pressure swing adsorption section is used for adsorbing oxygen in the oxygen-enriched mixed gas obtained in the step A of the adsorption tower of the first pressure swing adsorption section and improving the oxygen to more than 99.5% (V).
The dry air with the pressure of more than 5KPa enters an adsorption tower of the first pressure swing adsorption section in an adsorption step, the adsorbent in the adsorption tower selectively adsorbs components such as nitrogen in the air, components such as oxygen and argon which are not easy to adsorb are discharged from an outlet end to enter the adsorption tower of the second pressure swing adsorption section, the adsorbent in the adsorption tower selectively adsorbs components such as oxygen in oxygen-enriched mixed gas, the components such as nitrogen and argon which are not easy to adsorb flow out from the outlet end to enter the adsorption tower of the second section after vacuumizing, and the pressure is increased to the adsorption pressure and the oxygen is discharged after being adsorbed. After the adsorption of the adsorption tower of the first pressure swing adsorption section is finished, pressure equalizing is firstly carried out, then vacuum pumping is carried out, nitrogen and a small amount of oxygen are pumped out by a vacuum pump, after the adsorption of the adsorption tower of the second pressure swing adsorption section is finished, the product oxygen is firstly replaced, after the replacement is finished, vacuum pumping is carried out, a part of pumped high-concentration oxygen is used as a product to enter a pure oxygen buffer tank of the product after compression, and the other part of pumped high-concentration oxygen is used for replacing an adsorbent bed layer after the adsorption is finished. The concentration of oxygen in the outlet gas is controlled to be more than 70% (V) in the adsorption process of the adsorption tower of the first pressure swing adsorption section, and the adsorption tower sequentially undergoes four pressure swing adsorption process steps of adsorption A, pressure equalization and ED reduction, vacuumizing VC and pressure equalization and lifting in a cycle period; after the adsorption of the adsorption tower of the second pressure swing adsorption section is finished, the oxygen concentration in the outlet gas is controlled to be more than 60-70% (V), and the adsorption tower sequentially undergoes four pressure swing adsorption process steps of adsorption A, product oxygen replacement P, vacuumizing VC and serial adsorption A1 in a cycle period. The total recovery rate of oxygen is about 60%, the two-stage circulation time is generally 20-80 seconds, the first-stage vacuum degree is-0.07 MPa, and the air quantity of the air blower, the air tower speed of the two-stage adsorption tower, the air extraction quantity of the vacuum pump, the adsorbent consumption, the diameter of the adsorption tower and other design parameters are designed according to the common conditions in the pressure swing adsorption technical field.
Each adsorption tower of each section of the present invention is sequentially subjected to the following steps in one cycle.
Adsorption tower of first pressure swing adsorption section: each adsorption tower of the first section is sequentially subjected to the following steps in one cycle:
adsorption A
The method comprises the steps of opening a programmable valve KV1A-1, enabling dry air which is boosted to 5KPa to enter an adsorption tower T0101A for boosting, opening a programmable valve KV2A-1 when the pressure is boosted to the adsorption pressure, selectively and sequentially adsorbing components such as nitrogen in the air by an adsorbent in the adsorption tower, enabling components such as oxygen and argon which are not easy to adsorb to be discharged from an outlet end to enter an oxygen-enriched buffer tank V0201 by opening the programmable valve KV2A-1, controlling the oxygen-enriched concentration to be more than 70%, enabling the total amount of nitrogen adsorbed by the adsorbent to be increased continuously along with the time, stopping air inlet when the adsorbent is saturated by adsorbing nitrogen, and ending adsorption at the moment.
Equal pressure drop ED
After the adsorption step A is finished, a programmable valve KV3A-1 is opened, dead space gas in an adsorption tower T0101A is discharged from an outlet of the adsorption tower and enters an adsorption tower T0101B of which the vacuumizing step VC is finished, and the pressure of the adsorption tower T0101A are increased as much as possible.
Vacuum pumping VC
After the step of pressure drop ED of the adsorption tower T0101A is finished, a programmable valve KV4A-1 is opened, and nitrogen adsorbed in the adsorption tower T0101A is pumped out for emptying.
Equal-pressure rising ER
After the vacuumizing VC step of the adsorption tower T0101A is finished, a programmable valve KV3A-1 is opened, and the gas exhausted in the step of pressure drop ED of the adsorption tower T0101B is utilized to enter the adsorption tower T0101A from the outlet end of the adsorption tower T0101A, so that the pressure of the adsorption tower T0101A is increased, and the pressure of the adsorption tower T0101A and the pressure of the adsorption tower T0101B are equal to each other as much as possible.
After the steps, the adsorption tower T0101A completes a cycle, and enters the raw material gas again for adsorption, and the steps and the sequence of the other adsorption tower are identical to those of the adsorption tower T0101A, but are staggered in time.
Second pressure swing adsorption section
Adsorption A
Simultaneously, program control valves KV1A-2 and KV4A-2 of a second pressure swing adsorption section are opened, oxygen-enriched mixed gas obtained in the adsorption step A of the adsorption tower of the first pressure swing adsorption section enters an adsorbent bed layer of the adsorption tower T0201A from the bottom, adsorbents in the adsorption tower T0201A selectively enrich components such as oxygen and the like in the mixed gas, partial unadsorbed oxygen and tail gases such as nitrogen and argon which are not easy to adsorb flow out from an outlet end to enter the bottom of the adsorption tower T0201B for boosting, when the adsorption pressure is raised, program control valve KV2B-2 is opened, the unadsorbed nitrogen and argon are discharged from an outlet of the adsorption tower T0201B, the total amount of oxygen adsorbed by the adsorbents is continuously increased along with the time, and when the adsorption tower T0201A adsorbs oxygen to be saturated, air inlet is stopped, and the adsorption is finished at the moment. And (3) after the adsorption step A of the adsorption tower is finished, controlling the oxygen concentration in the outlet gas to be 60-70% (V).
Product oxygen displacement P
After the adsorption step A is finished, the program control valves KV1A-2, KV4A-2 and KV2B-2 are closed, the program control valves KV3A-2 and KV6A-2 are opened, product oxygen enters the top of an adsorbent bed from the bottom of the adsorption tower T0201A and flows out, and the mixed gas flowing out from the top returns to the inlet of the first pressure swing adsorption section and is mixed with the oxygen-enriched mixed gas obtained in the adsorption step A of the adsorption tower of the first pressure swing adsorption section and then enters the adsorption tower of the second pressure swing adsorption section as raw material gas for adsorption. After the P step of oxygen replacement of the adsorption tower product is finished, the oxygen concentration in the outlet gas is controlled to be more than 98% (V).
Vacuum pumping VC
After the oxygen replacement P of the product of the adsorption tower T0201A is finished, closing the programmable valves KV3A-2 and KV6A-2, opening the programmable valve KV5A-2, pumping out the oxygen adsorbed by the adsorbent from the bottom of the adsorption tower by using a vacuum pump, wherein one part of the oxygen is taken as the product oxygen, and the other part of the oxygen is taken as the replacement gas to return to replace the adsorbent bed.
Series adsorption A1
After the vacuumizing VC of the adsorption tower T0201A is finished, closing a programmable valve KV5A-2, opening the programmable valves KV1D-2, KV4D-2 and KV2A-2, mixing oxygen-enriched raw material gas with tail gas flowing out of the top after the oxygen replacement of the product of the adsorption tower T0201C, enabling the mixed gas to enter an adsorbent bed layer of the adsorption tower T0201D to adsorb oxygen, enabling the tail gas to enter the adsorption tower T0201A through the programmable valve KV4D-2 to boost pressure and adsorb oxygen, enabling nitrogen and argon which are not easy to adsorb and a small amount of oxygen to be exhausted through the programmable valve KV2A-2, and closing the programmable valves KV1D-2, KV4D-2 and KV2A-2 after the serial connection adsorption of the adsorption towers T0201D and T0201A is finished. In the step of A1 adsorption by the adsorption towers in series, the oxygen concentration in the outlet gas is controlled at 20-40% (V).
After the steps, the adsorption tower T0201A completes a cycle, and enters the oxygen-enriched raw material gas again for adsorption, and the steps and the sequence of the other three adsorption towers are identical to those of the adsorption tower T0201A, but are staggered in time.
Example 2:
FIG. 3 is a timing chart showing the operation steps of the adsorption tower and the switching of the programmable valve according to the embodiment 2 of the present invention.
Fig. 4 is a process flow diagram of embodiment 2 of the present invention.
The raw material air composition of this example is as follows:
| the components | O 2 | N 2 | Ar | CO 2 | Others | ∑ |
| Concentration (%) (V) | 20.93 | 78.03 | 0.932 | 0.03 | 0.078 | 100 |
Temperature: the temperature is less than or equal to 40 DEG C
Pressure: 0.05MPa (G)
As shown in fig. 4, a first pressure swing adsorption section is formed by a vacuum pump P0101, a vacuum buffer tank V0101, a program-controlled valve, a PLC control system, instruments and meters, process pipeline pipes, adsorption towers T0101A and T0101B, and the adsorbent filled in the adsorption towers is a 5A molecular sieve or a lithium molecular sieve, so that a single-tower adsorption, pressure equalizing and vacuumizing procedure is operated; pure oxygen vacuum pump P0201, pure oxygen compressor C0201, oxygen boosting buffer tank V0201, compressor buffer tank V0202, product pure oxygen buffer tank V0203, program control valve, PLC control system, instrument and meter, process pipeline pipe fitting, adsorption tower T0201A, T0201B, T0201C, T0201D and T0201E constitute the second pressure swing adsorption section, and the adsorbent that fills in the adsorption tower is carbon molecular sieve, operation single tower series connection adsorption, series connection replacement and evacuation procedure. In this embodiment, the two sections of pressure swing adsorption are operated in series, the first pressure swing adsorption section adsorbs nitrogen in air, and the second pressure swing adsorption section is used for adsorbing oxygen in the oxygen-enriched mixed gas obtained in the step A of the adsorption tower of the first pressure swing adsorption section and improving the oxygen to more than 99.5% (V).
The dry air with the pressure of more than 5KPa enters an adsorption tower of the first pressure swing adsorption section in an adsorption step, the adsorbent in the adsorption tower selectively adsorbs components such as nitrogen in the air, components such as oxygen and argon which are not easy to adsorb are discharged from an outlet end to enter the adsorption tower of the second pressure swing adsorption section, the adsorbent in the adsorption tower selectively adsorbs components such as oxygen in oxygen-enriched mixed gas, the components such as nitrogen and argon which are not easy to adsorb flow out from the outlet end to enter the adsorption tower of the second section after vacuumizing, and the pressure is increased to the adsorption pressure and the oxygen is discharged after being adsorbed. After the adsorption of the adsorption tower of the first pressure swing adsorption section is finished, pressure equalizing and vacuumizing are carried out, nitrogen and a small amount of oxygen pumped by a vacuum pump are exhausted, the concentration of oxygen in outlet gas in the adsorption process of the adsorption tower is controlled to be more than 70% (V), and the adsorption tower sequentially undergoes four pressure swing adsorption process steps of adsorption A, pressure equalizing and ED reducing, vacuumizing and VC and pressure equalizing and lifting in a cycle period; the concentration of oxygen in the outlet gas of the adsorption tower of the second pressure swing adsorption section in the adsorption step is controlled to be close to the concentration of oxygen in the raw material gas, and the adsorption tower sequentially undergoes five pressure swing adsorption process steps of adsorption A, serial replacement P1, product oxygen replacement P, vacuumizing VC and serial adsorption A1 in one cycle period. The total recovery rate of oxygen is about 60%, the two-stage circulation time is generally 20-80 seconds, the first-stage vacuum degree is-0.07 MPa, and the air quantity of the air blower, the air tower speed of the two-stage adsorption tower, the air extraction quantity of the vacuum pump, the adsorbent consumption, the diameter of the adsorption tower and other design parameters are designed according to the common conditions in the pressure swing adsorption technical field.
Each adsorption tower of each section of the present invention is sequentially subjected to the following steps in one cycle.
Adsorption tower of first pressure swing adsorption section: each adsorption tower of the first section is sequentially subjected to the following steps in one cycle:
adsorption A
The method comprises the steps of opening a programmable valve KV1A-1, enabling dry air which is boosted to 5KPa to enter an adsorption tower T0101A for boosting, opening a programmable valve KV2A-1 when the pressure is boosted to the adsorption pressure, selectively and sequentially adsorbing components such as nitrogen in the air by an adsorbent in the adsorption tower, enabling components such as oxygen and argon which are not easy to adsorb to be discharged from an outlet end to enter an oxygen-enriched buffer tank V0201 by opening the programmable valve KV2A-1, controlling the oxygen-enriched concentration to be more than 70%, enabling the total amount of nitrogen adsorbed by the adsorbent to be increased continuously along with the time, stopping air inlet when the adsorbent is saturated by adsorbing nitrogen, and ending adsorption at the moment.
Equal pressure drop ED
After the adsorption step A is finished, a programmable valve KV3A-1 is opened, dead space gas in an adsorption tower T0101A is discharged from an outlet of the adsorption tower and enters an adsorption tower T0101B of which the vacuumizing step VC is finished, and the pressure of the adsorption tower T0101A are increased as much as possible.
Vacuum pumping VC
After the step of pressure drop ED of the adsorption tower T0101A is finished, a programmable valve KV4A-1 is opened, and nitrogen adsorbed in the adsorption tower T0101A is pumped out for emptying.
Equal-pressure rising ER
After the vacuumizing VC step of the adsorption tower T0101A is finished, a programmable valve KV3A-1 is opened, and the gas exhausted in the step of pressure drop ED of the adsorption tower T0101B is utilized to enter the adsorption tower T0101A from the outlet end of the adsorption tower T0101A, so that the pressure of the adsorption tower T0101A is increased, and the pressure of the adsorption tower T0101A and the pressure of the adsorption tower T0101B are equal to each other as much as possible.
After the steps, the adsorption tower T0101A completes a cycle, and enters the raw material gas again for adsorption, and the steps and the sequence of the other adsorption tower are identical to those of the adsorption tower T0101A, but are staggered in time.
Second pressure swing adsorption section
Adsorption A
Simultaneously, program control valves KV1A-2 and KV4A-2 of a second pressure swing adsorption section are opened, oxygen-enriched mixed gas obtained in the adsorption step A of the adsorption tower of the first pressure swing adsorption section enters an adsorbent bed layer of the adsorption tower T0201A from the bottom, adsorbents in the adsorption tower T0201A selectively enrich components such as oxygen and the like in the mixed gas, partial unadsorbed oxygen and tail gases such as nitrogen and argon which are not easy to adsorb flow out from an outlet end to enter the bottom of the adsorption tower T0201B for boosting, when the adsorption pressure is raised, program control valve KV2B-2 is opened, the unadsorbed nitrogen and argon are discharged from an outlet of the adsorption tower T0201B, the total amount of the adsorbent adsorbed oxygen is continuously increased along with the time, and when the adsorption tower T0201A is saturated with the adsorbed oxygen, air inlet is stopped, and the adsorption is ended at the moment. And (3) after the adsorption step A of the adsorption tower is finished, controlling the oxygen concentration in the outlet gas to be 60-70% (V).
Second-order serial replacement P1
After the adsorption step A is finished, the program control valves KV1A-2, KV4A-2 and KV2B-2 are closed, the program control valves KV6E-2, KV3E-2 and KV2A-2 are opened, product oxygen enters an adsorbent bed from the bottom of the adsorption tower T0201E to replace nitrogen and argon, then flows out from the top, replacement tail gas flowing out from the top enters the bottom of the adsorption tower T0201A, and after the oxygen is adsorbed by the adsorbent bed of the adsorption tower T0201A, the oxygen is returned to the inlet of the second section through the program control valve KV2A-2 to be mixed with oxygen-enriched gas obtained in the adsorption step of the adsorption tower of the first pressure swing adsorption section. After the P1 replacement step of the adsorption towers in series connection is finished, the oxygen concentration in the outlet gas is controlled at 60-80% (V).
Third step of product oxygen substitution P
After the step of serial replacement P1 is finished, program control valves KV6E-2, KV3E-2 and KV2A-2 are closed, program control valves KV3A-2 and KV6A-2 are opened, product oxygen enters an adsorbent bed from the bottom of an adsorption tower T0201A to replace nitrogen and argon, then flows out from the top, replacement tail gas flowing out from the top enters from the bottom of an adsorption tower T0201B, and after the oxygen is adsorbed by the adsorbent bed of the adsorption tower T0201B, the oxygen is exhausted through the program control valve KV 2B-2. After the P step of oxygen replacement of the adsorption tower product is finished, the oxygen concentration in the outlet gas is controlled to be more than 98% (V).
Vacuum-pumping VC
After the oxygen replacement P of the product of the adsorption tower T0201A is finished, closing the programmable valves KV3A-2 and KV6A-2, opening the programmable valve KV5A-2, pumping out the oxygen adsorbed by the adsorbent from the bottom of the adsorption tower by using a vacuum pump, wherein one part of the oxygen is taken as the product oxygen, and the other part of the oxygen is taken as the replacement gas to return to replace the adsorbent bed.
Series adsorption A1
After the vacuumizing VC of the adsorption tower T0201A is finished, closing a programmable valve KV5A-2, opening programmable valves KV1E-2, KV4E-2 and KV7A-2, enabling oxygen-enriched raw material gas to enter an adsorbent bed layer of the adsorption tower T0201E to adsorb oxygen, enabling tail gas to enter the adsorption tower T0201A through the programmable valve KV4E-2 to boost pressure and adsorb oxygen, and closing the programmable valves KV1E-2, KV4E-2 and KV7A-2 after the serial connection adsorption of the adsorption tower T0201E and the adsorption of the adsorption tower T0201A is finished.
After the steps, the adsorption tower T0201A completes a cycle, and enters the oxygen-enriched raw material gas again for adsorption, and the steps and the sequence of the other four adsorption towers are identical to those of the adsorption tower T0201A, but are staggered in time.
Example 3:
FIG. 5 is a timing chart showing the operation steps of the adsorption tower and the switching of the programmable valve in each section of embodiment 3 of the present invention.
Fig. 6 is a process flow diagram of example 3 of the present invention.
The raw material air composition of this example is as follows:
| the components | O 2 | N 2 | Ar | CO 2 | Others | ∑ |
| Concentration (%) (V) | 20.93 | 78.03 | 0.932 | 0.03 | 0.078 | 100 |
Temperature: the temperature is less than or equal to 40 DEG C
Pressure: 0.05MPa (G)
As shown in fig. 6, a vacuum pump P0101, a vacuum buffer tank V0101, a program-controlled valve, a PLC control system, instruments and meters, process pipeline pipes, and adsorption towers T0101A, T0101B and T0101C form a first pressure swing adsorption section, the adsorbent filled in the adsorption towers is a 5A molecular sieve or a lithium molecular sieve, and a single-tower adsorption, pressure equalizing and vacuumizing procedure is operated; pure oxygen vacuum pump P0201, pure oxygen compressor C0201, compressor buffer tank V0202, product pure oxygen buffer tank V0203, program control valve, PLC control system, instrument and meter, process pipe fitting, adsorption tower T0201A, T0201B, T0201C and T0201D constitute the second pressure swing adsorption section, and the adsorbent of packing in the adsorption tower is carbon molecular sieve, operation single tower adsorption, displacement and evacuation procedure. In this embodiment, the two sections of pressure swing adsorption are operated in series, the first pressure swing adsorption section adsorbs nitrogen in air, and the second pressure swing adsorption section is used for adsorbing oxygen in the oxygen-enriched mixed gas obtained in the step A of the adsorption tower of the first pressure swing adsorption section and improving the oxygen to more than 99.5% (V).
The dry air with the pressure of more than 5KPa enters an adsorption tower of the first pressure swing adsorption section in an adsorption step, the adsorbent in the adsorption tower selectively adsorbs components such as nitrogen in the air, components such as oxygen and argon which are not easy to adsorb are discharged from an outlet end to enter the adsorption tower of the second pressure swing adsorption section, the adsorbent in the adsorption tower selectively adsorbs components such as oxygen in oxygen-enriched mixed gas, the components such as nitrogen and argon which are not easy to adsorb flow out from the outlet end to enter the adsorption tower of the second section after vacuumizing, and the pressure is increased to the adsorption pressure and the oxygen is discharged after being adsorbed. After the adsorption of the adsorption tower of the first pressure swing adsorption section is finished, pressure equalizing is firstly carried out, then vacuum pumping is carried out, nitrogen and a small amount of oxygen are pumped out by a vacuum pump, after the adsorption of the adsorption tower of the second pressure swing adsorption section is finished, the product oxygen is firstly replaced, after the replacement is finished, vacuum pumping is carried out, a part of pumped high-concentration oxygen is used as a product to enter a pure oxygen buffer tank of the product after compression, and the other part of pumped high-concentration oxygen is used for replacing an adsorbent bed layer after the adsorption is finished. The concentration of oxygen in the outlet gas is controlled to be more than 70% (V) in the adsorption process of the adsorption tower of the first pressure swing adsorption section, and the adsorption tower sequentially undergoes five pressure swing adsorption process steps of adsorption A, pressure equalizing and reducing ED, vacuumizing VC, pressure equalizing and lifting ER and repressing FR in a cycle period; after the adsorption of the adsorption tower of the second pressure swing adsorption section is finished, the oxygen concentration in the outlet gas is controlled to be more than 60-70% (V), and the adsorption tower sequentially undergoes four pressure swing adsorption process steps of adsorption A, product oxygen replacement P, vacuumizing VC and serial adsorption A1 in a cycle period. The total recovery rate of oxygen is about 60%, the two-stage circulation time is generally 20-80 seconds, the first-stage vacuum degree is-0.07 MPa, and the air quantity of the air blower, the air tower speed of the two-stage adsorption tower, the air extraction quantity of the vacuum pump, the adsorbent consumption, the diameter of the adsorption tower and other design parameters are designed according to the common conditions in the pressure swing adsorption technical field.
Each adsorption tower of each section of the present invention is sequentially subjected to the following steps in one cycle.
Adsorption tower of first pressure swing adsorption section: each adsorption tower of the first section is sequentially subjected to the following steps in one cycle:
adsorption A
And opening program control valves KV1A-1 and KV2A-1 of the first pressure swing adsorption section, enabling dry air to enter an adsorbent bed layer of an adsorption tower T0101A from the bottom, enabling an adsorbent in the adsorption tower T0101A to selectively adsorb nitrogen and other components, enabling non-adsorbed partial nitrogen and components such as oxygen and argon which are not easy to adsorb to flow out from an outlet end and enter an adsorption tower of the second pressure swing adsorption section in an adsorption step, enabling the total amount of the components such as nitrogen adsorbed by the adsorbent to be continuously increased along with the time, stopping air inlet when the adsorption tower T0101A is saturated with the adsorbed nitrogen, and ending adsorption at the moment. In the process of the adsorption step A of the adsorption tower, the oxygen concentration in the outlet gas is controlled to be more than 70% (V).
Equal pressure drop ED
After the adsorption step A is finished, the programmable valves KV3A-1 and KV3C-1 are opened, dead space gas in the adsorption tower T0101A is discharged from an outlet of the adsorption tower and enters the adsorption tower T0101C of which the vacuumizing step VC is finished, and the pressure of the two towers is increased as much as possible.
Vacuum pumping VC
After the pressure drop ED of the adsorption tower T0101A is finished, the program control valve KV4A-1 is opened, nitrogen adsorbed in the adsorption tower T0101A is pumped out for emptying, and the adsorbent is regenerated.
Equal-pressure rising ER
After the vacuumizing VC step of the adsorption tower T0101A is finished, opening a program control valve KV3A-1 and a program control valve KV3B-1, and enabling the gas discharged in the step of reducing the pressure ED of the adsorption tower T0101B to enter the adsorption tower from the outlet end of the adsorption tower T0101A so as to enable the pressure of the adsorption tower T0101A to be increased, so that the pressure of the adsorption tower T0101A is equal to the pressure of the adsorption tower T0101B as much as possible.
Final boost FR
After the end of the pressure equalization and ER rising, closing the programmable valve KV3A-1, opening the programmable valve KV2A-1, and using the outlet gas in the adsorption process to boost the adsorption tower T0101A until the adsorption pressure approaches to the adsorption pressure of the first pressure swing adsorption section.
After the steps, the adsorption tower T0101A completes a cycle, and enters the raw material gas again for adsorption, and the steps and the sequence of the other adsorption tower are identical to those of the adsorption tower T0101A, but are staggered in time.
Second pressure swing adsorption section
Adsorption A
Simultaneously, program control valves KV1A-2 and KV4A-2 of a second pressure swing adsorption section are opened, oxygen-enriched mixed gas obtained in the adsorption step A of the adsorption tower of the first pressure swing adsorption section enters an adsorbent bed layer of the adsorption tower T0201A from the bottom, adsorbents in the adsorption tower T0201A selectively enrich components such as oxygen and the like in the mixed gas, partial unadsorbed oxygen and tail gases such as nitrogen and argon which are not easy to adsorb flow out from an outlet end to enter the bottom of the adsorption tower T0201B for boosting, when the adsorption pressure is raised, program control valve KV2B-2 is opened, the unadsorbed nitrogen and argon are discharged from an outlet of the adsorption tower T0201B, the total amount of oxygen adsorbed by the adsorbents is continuously increased along with the time, and when the adsorption tower T0201A adsorbs oxygen to be saturated, air inlet is stopped, and the adsorption is finished at the moment. And (3) after the adsorption step A of the adsorption tower is finished, controlling the oxygen concentration in the outlet gas to be 60-70% (V).
Product oxygen displacement P
After the adsorption step A is finished, the program control valves KV1A-2, KV4A-2 and KV2B-2 are closed, the program control valves KV3A-2 and KV6A-2 are opened, product oxygen enters the top of an adsorbent bed from the bottom of the adsorption tower T0201A and flows out, and the mixed gas flowing out from the top returns to the inlet of the first pressure swing adsorption section and is mixed with the oxygen-enriched mixed gas obtained in the adsorption step A of the adsorption tower of the first pressure swing adsorption section and then enters the adsorption tower of the second pressure swing adsorption section as raw material gas for adsorption. After the P step of oxygen replacement of the adsorption tower product is finished, the oxygen concentration in the outlet gas is controlled to be more than 98% (V).
Vacuum pumping VC
After the oxygen replacement P of the product of the adsorption tower T0201A is finished, closing the programmable valves KV3A-2 and KV6A-2, opening the programmable valve KV5A-2, pumping out the oxygen adsorbed by the adsorbent from the bottom of the adsorption tower by using a vacuum pump, wherein one part of the oxygen is taken as the product oxygen, and the other part of the oxygen is taken as the replacement gas to return to replace the adsorbent bed.
Series adsorption A1
After the vacuumizing VC of the adsorption tower T0201A is finished, closing a programmable valve KV5A-2, opening the programmable valves KV1D-2, KV4D-2 and KV2A-2, mixing oxygen-enriched raw material gas with tail gas flowing out of the top after the oxygen replacement of the product of the adsorption tower T0201C, enabling the mixed gas to enter an adsorbent bed layer of the adsorption tower T0201D to adsorb oxygen, enabling the tail gas to enter the adsorption tower T0201A through the programmable valve KV4D-2 to boost pressure and adsorb oxygen, enabling nitrogen and argon which are not easy to adsorb and a small amount of oxygen to be exhausted through the programmable valve KV2A-2, and closing the programmable valves KV1D-2, KV4D-2 and KV2A-2 after the serial connection adsorption of the adsorption towers T0201D and T0201A is finished. In the step of A1 adsorption by the adsorption towers in series, the oxygen concentration in the outlet gas is controlled at 20-40% (V).
After the steps, the adsorption tower T0201A completes a cycle, and enters the oxygen-enriched raw material gas again for adsorption, and the steps and the sequence of the other three adsorption towers are identical to those of the adsorption tower T0201A, but are staggered in time.
Example 4:
FIG. 7 is a timing chart showing the operation steps of the adsorption tower and the switching of the programmable valve according to the embodiment 4 of the present invention.
Fig. 8 is a process flow diagram of example 4 of the present invention.
The raw material air composition of this example is as follows:
| the components | O 2 | N 2 | Ar | CO 2 | Others | ∑ |
| Concentration (%) (V) | 20.93 | 78.03 | 0.932 | 0.03 | 0.078 | 100 |
Temperature: the temperature is less than or equal to 40 DEG C
Pressure: 0.05MPa (G)
As shown in fig. 8, a drying section is formed by a blower C0100, a program control valve, a PLC control system, instruments, process pipeline pipes, an adsorption tower T0100A and T0100B for pressure swing adsorption, an adsorbent filled in the adsorption tower is an activated alumina desiccant, and a single-tower adsorption and purge regeneration program is operated; the vacuum pump P0101, the vacuum buffer tank V0101, the program control valve, the PLC control system, the instrument and the instrument, the process pipeline pipe fitting, the adsorption towers T0101A and T0101B form a first pressure swing adsorption section, the adsorbent filled in the adsorption towers is a 5A molecular sieve or a lithium molecular sieve, and single-tower adsorption, pressure equalizing and vacuumizing procedures are operated; pure oxygen vacuum pump P0201, pure oxygen compressor C0201, oxygen boosting buffer tank V0201, compressor buffer tank V0202, product pure oxygen buffer tank V0203, program control valve, PLC control system, instrument and meter, process pipeline pipe fitting, adsorption tower T0201A, T0201B, T0201C and T0201D constitute the second pressure swing adsorption section, and the adsorbent that packs in the adsorption tower is carbon molecular sieve, operation single tower adsorption, displacement and evacuation procedure. In this embodiment, the three sections of pressure swing adsorption are operated in series, the drying section pressure swing adsorption is used for adsorbing gaseous water in air, so as to meet the requirement of the pressure swing adsorption oxygen-making adsorbent on water, the first pressure swing adsorption section adsorbs nitrogen in air, the second pressure swing adsorption section is used for adsorbing oxygen in the oxygen-enriched mixed gas obtained in the step A of the first pressure swing adsorption section adsorption tower, and the oxygen is improved to more than 99.5% (V).
The air is boosted to 5KPa by a blower C0100 and then enters a drying section for pressure swing adsorption, the adsorbent in the adsorption tower selectively adsorbs components such as gaseous water in wet air, components such as oxygen, nitrogen and argon which are difficult to adsorb enter the adsorption tower of the first pressure swing adsorption section in an adsorption step from an outlet end, the adsorbent in the adsorption tower selectively adsorbs components such as nitrogen in air, the components such as oxygen and argon which are difficult to adsorb are discharged from the outlet end into the adsorption tower of the second pressure swing adsorption section, the adsorbent in the adsorption tower selectively adsorbs components such as oxygen in oxygen-enriched mixed gas, the components such as nitrogen and argon which are difficult to adsorb flow out from the outlet end into the adsorption tower of the second section for boosting and adsorbing oxygen, and the components such as nitrogen and argon which are difficult to adsorb are discharged after boosting to the adsorption pressure and adsorbing oxygen. After the adsorption of the adsorption tower of the first pressure swing adsorption section is finished, pressure equalizing is firstly carried out, then vacuum pumping is carried out, nitrogen and a small amount of oxygen are pumped out by a vacuum pump, after the adsorption of the adsorption tower of the second pressure swing adsorption section is finished, the product oxygen is firstly replaced, after the replacement is finished, vacuum pumping is carried out, a part of pumped high-concentration oxygen is used as a product to enter a pure oxygen buffer tank of the product after compression, and the other part of pumped high-concentration oxygen is used for replacing an adsorbent bed layer after the adsorption is finished. The drying section pressure swing adsorption is used for controlling the dew point of the wet air to be more than minus 50 ℃, and an adsorption tower of the drying section pressure swing adsorption sequentially undergoes two pressure swing adsorption process steps of adsorption A and purging P in a cycle period; the concentration of oxygen in the outlet gas is controlled to be more than 70% (V) in the adsorption process of the adsorption tower of the first pressure swing adsorption section, and the adsorption tower sequentially undergoes four pressure swing adsorption process steps of adsorption A, pressure equalization and ED reduction, vacuumizing VC and pressure equalization and lifting in a cycle period; after the adsorption of the adsorption tower of the second pressure swing adsorption section is finished, the oxygen concentration in the outlet gas is controlled to be more than 60-70% (V), and the adsorption tower sequentially undergoes four pressure swing adsorption process steps of adsorption A, product oxygen replacement P, vacuumizing VC and serial adsorption A1 in a cycle period. The total recovery rate of oxygen is about 60%, the three-stage circulation time is generally 20-80 seconds, the first-stage vacuum degree is-0.07 MPa, the air quantity of a blower, the air tower speed of the three-stage adsorption tower, the air extraction quantity of a vacuum pump, the consumption of the adsorbent, the diameter of the adsorption tower and other design parameters are designed according to the common conditions in the pressure swing adsorption technical field.
Each adsorption tower of each section of the present invention is sequentially subjected to the following steps in one cycle.
Pressure swing adsorption drying section
Adsorption A
After the program control valves KV1A-0 and KV2A-0 are opened, raw material air is boosted to 5KPa (G) through a blower (C0101), then enters an active alumina bed layer from the bottom of an adsorption tower T0100A, gaseous water in the air is adsorbed, components such as oxygen, nitrogen and argon which are not easy to adsorb are discharged from an outlet end and enter the bottom of an adsorption tower of a first pressure swing adsorption section, as time goes on, the total amount of gaseous water adsorbed by the active alumina is continuously increased, when the active alumina is saturated with the gaseous water, air inlet is stopped, adsorption is finished at the moment, and the dew point of the outlet mixed gas in the adsorption step A of a pressure swing adsorption drying section is controlled to be about 50 ℃.
Purges the second place
After the adsorption of the adsorption tower T0100A is finished, the programmable valves KV3A-0 and KV4A-0 are opened, the vent air of the adsorption tower adsorption A step of the first pressure swing adsorption section and the vent air of the adsorption tower air adsorption A2 step of the tail gas adsorption A1 step of the second pressure swing adsorption section enter the adsorption tower from the outlet end of the adsorption tower T0100A through the programmable valve KV3A-0, then the vent air is discharged from the bottom of the adsorption tower T0100A through the programmable valve KV4A-0, and after the purging P is finished, the programmable valves KV3A-0 and KV4A-0 are closed.
After the steps, the adsorption tower T0100A completes a cycle, and enters dry air again for adsorption, and the steps and the sequence of the other adsorption tower are identical to those of the adsorption tower T0100A, but are staggered in time.
Adsorption tower of first pressure swing adsorption section: each adsorption tower of the first section is sequentially subjected to the following steps in one cycle:
adsorption A
The method comprises the steps of opening a programmable valve KV1A-1, enabling dry air which is boosted to 5KPa to enter an adsorption tower T0101A for boosting, opening a programmable valve KV2A-1 when the pressure is boosted to the adsorption pressure, selectively and sequentially adsorbing components such as nitrogen in the air by an adsorbent in the adsorption tower, enabling components such as oxygen and argon which are not easy to adsorb to be discharged from an outlet end to enter an oxygen-enriched buffer tank V0201 by opening the programmable valve KV2A-1, controlling the oxygen-enriched concentration to be more than 70%, enabling the total amount of nitrogen adsorbed by the adsorbent to be increased continuously along with the time, stopping air inlet when the adsorbent is saturated by adsorbing nitrogen, and ending adsorption at the moment.
Equal pressure drop ED
After the adsorption step A is finished, a programmable valve KV3A-1 is opened, dead space gas in an adsorption tower T0101A is discharged from an outlet of the adsorption tower and enters an adsorption tower T0101B of which the vacuumizing step VC is finished, and the pressure of the adsorption tower T0101A are increased as much as possible.
Vacuum pumping VC
After the step of pressure drop ED of the adsorption tower T0101A is finished, a programmable valve KV4A-1 is opened, and nitrogen adsorbed in the adsorption tower T0101A is pumped out for emptying.
Equal-pressure rising ER
After the vacuumizing VC step of the adsorption tower T0101A is finished, a programmable valve KV3A-1 is opened, and the gas exhausted in the step of pressure drop ED of the adsorption tower T0101B is utilized to enter the adsorption tower T0101A from the outlet end of the adsorption tower T0101A, so that the pressure of the adsorption tower T0101A is increased, and the pressure of the adsorption tower T0101A and the pressure of the adsorption tower T0101B are equal to each other as much as possible.
After the steps, the adsorption tower T0101A completes a cycle, and enters the raw material gas again for adsorption, and the steps and the sequence of the other adsorption tower are identical to those of the adsorption tower T0101A, but are staggered in time.
Second pressure swing adsorption section
Adsorption A
Simultaneously, program control valves KV1A-2 and KV4A-2 of a second pressure swing adsorption section are opened, oxygen-enriched mixed gas obtained in the adsorption step A of the adsorption tower of the first pressure swing adsorption section enters an adsorbent bed layer of the adsorption tower T0201A from the bottom, adsorbents in the adsorption tower T0201A selectively enrich components such as oxygen and the like in the mixed gas, partial unadsorbed oxygen and tail gases such as nitrogen and argon which are not easy to adsorb flow out from an outlet end to enter the bottom of the adsorption tower T0201B for boosting, when the adsorption pressure is raised, program control valve KV2B-2 is opened, the unadsorbed nitrogen and argon are discharged from an outlet of the adsorption tower T0201B, the total amount of oxygen adsorbed by the adsorbents is continuously increased along with the time, and when the adsorption tower T0201A adsorbs oxygen to be saturated, air inlet is stopped, and the adsorption is finished at the moment. And (3) after the adsorption step A of the adsorption tower is finished, controlling the oxygen concentration in the outlet gas to be 60-70% (V).
Product oxygen displacement P
After the adsorption step A is finished, the program control valves KV1A-2, KV4A-2 and KV2B-2 are closed, the program control valves KV3A-2 and KV6A-2 are opened, product oxygen enters the top of an adsorbent bed from the bottom of the adsorption tower T0201A and flows out, and the mixed gas flowing out from the top returns to the inlet of the first pressure swing adsorption section and is mixed with the oxygen-enriched mixed gas obtained in the adsorption step A of the adsorption tower of the first pressure swing adsorption section and then enters the adsorption tower of the second pressure swing adsorption section as raw material gas for adsorption. After the P step of oxygen replacement of the adsorption tower product is finished, the oxygen concentration in the outlet gas is controlled to be more than 98% (V).
Vacuum pumping VC
After the oxygen replacement P of the product of the adsorption tower T0201A is finished, closing the programmable valves KV3A-2 and KV6A-2, opening the programmable valve KV5A-2, pumping out the oxygen adsorbed by the adsorbent from the bottom of the adsorption tower by using a vacuum pump, wherein one part of the oxygen is taken as the product oxygen, and the other part of the oxygen is taken as the replacement gas to return to replace the adsorbent bed.
Series adsorption A1
After the vacuumizing VC of the adsorption tower T0201A is finished, closing a programmable valve KV5A-2, opening the programmable valves KV1D-2, KV4D-2 and KV2A-2, mixing oxygen-enriched raw material gas with tail gas flowing out of the top after the oxygen replacement of the product of the adsorption tower T0201C, enabling the mixed gas to enter an adsorbent bed layer of the adsorption tower T0201D to adsorb oxygen, enabling the tail gas to enter the adsorption tower T0201A through the programmable valve KV4D-2 to boost pressure and adsorb oxygen, enabling nitrogen and argon which are not easy to adsorb and a small amount of oxygen to be exhausted through the programmable valve KV2A-2, and closing the programmable valves KV1D-2, KV4D-2 and KV2A-2 after the serial connection adsorption of the adsorption towers T0201D and T0201A is finished. In the step of A1 adsorption by the adsorption towers in series, the oxygen concentration in the outlet gas is controlled at 20-40% (V).
After the steps, the adsorption tower T0201A completes a cycle, and enters the oxygen-enriched raw material gas again for adsorption, and the steps and the sequence of the other three adsorption towers are identical to those of the adsorption tower T0201A, but are staggered in time.
Claims (9)
1. A method for a mobile pressure swing adsorption oxygen production device is characterized by comprising a first pressure swing adsorption section and a second pressure swing adsorption section which are operated in series, wherein dry raw material air firstly enters a nitrogen balance selective adsorbent bed in an adsorption tower of the first pressure swing adsorption section, so that most of nitrogen is adsorbed by the nitrogen balance selective adsorbent bed, most of oxygen and argon flow into an adsorption tower of the second pressure swing adsorption section from an outlet of the adsorption tower, and the oxygen in an oxygen-enriched mixed gas is adsorbed by the speed selective adsorbent bed of the second pressure swing adsorption section through a speed selective adsorbent bed of the second pressure swing adsorption section, and the nitrogen, the argon and a small amount of oxygen flow out from an outlet of the adsorption tower, and the mixed gas resolved by the second pressure swing adsorption section is high-concentration oxygen; the adsorption tower of the first pressure swing adsorption section sequentially undergoes at least four pressure swing adsorption process steps of adsorption A, pressure equalizing drop ED, reverse discharge BD or vacuumizing VC and pressure equalizing rise ER in a cycle period; the adsorption tower of the second pressure swing adsorption section is at least sequentially subjected to the pressure swing adsorption process steps of adsorption A, product oxygen replacement P, vacuumizing VC and serial adsorption A1 in a cycle period, wherein the serial adsorption A1 is obtained by mixing oxygen-enriched mixed gas obtained in the adsorption tower adsorption A step of the first pressure swing adsorption section with oxygen-enriched mixed gas flowing out of an outlet of an adsorption tower positioned in the product oxygen replacement P step in the second pressure swing adsorption section, the oxygen-enriched mixed gas enters the adsorption tower positioned in the adsorption A step in the second pressure swing adsorption section to adsorb oxygen, tail gas enters the adsorption tower in the second pressure swing adsorption section to complete the vacuumizing VC step to boost and adsorb the oxygen, and nitrogen and argon which are difficult to adsorb and a small amount of oxygen are discharged from the top of the adsorption tower.
2. The method of a mobile pressure swing adsorption oxygen plant according to claim 1, wherein the adsorption column of the second pressure swing adsorption stage is followed by a serial displacement P1 step, the displacement gas of the serial displacement P1 step being derived from the mixture gas discharged from the outlet of another adsorption column in the product oxygen displacement P step.
3. The method of a mobile pressure swing adsorption oxygen production plant according to claim 1 or 2 wherein the adsorption column of the first pressure swing adsorption stage is followed by a final pressure boost FR step of the pressure boost from the oxygen-enriched mixture at the outlet of the adsorption column adsorption a step of the first stage.
4. The method of a mobile pressure swing adsorption oxygen production plant according to claim 1 or 2, wherein the bottom of the adsorption column of the first pressure swing adsorption section is filled with a desiccant, the upper part is filled with a nitrogen balance selective adsorbent bed, raw material air containing gaseous water enters from the bottom of the adsorption column of the first pressure swing adsorption section and sequentially passes through the desiccant bed and the nitrogen balance selective adsorbent bed, most of the gaseous water in the raw material air is adsorbed by the desiccant bed, most of the nitrogen is adsorbed by the nitrogen balance selective adsorbent bed, most of the oxygen and argon flow out from the outlet of the adsorption column and enter the speed selective adsorbent bed of the second pressure swing adsorption section from the bottom of the adsorption column of the second pressure swing adsorption section, oxygen in the oxygen-enriched mixture is adsorbed by the speed selective adsorbent bed, nitrogen and argon flow out from the outlet of the adsorption column, and the desorbed mixture is high-concentration oxygen.
5. The method of a mobile pressure swing adsorption oxygen production plant according to claim 1 or 2, wherein the pressure of the adsorption a step of the adsorption towers of the first pressure swing adsorption section and the second pressure swing adsorption section is 0.005-0.2MPa, which is gauge pressure.
6. The method of a mobile pressure swing adsorption oxygen production plant according to claim 1 or 2, wherein the concentration of oxygen in the outlet gas at the end of adsorption a step of the adsorption column of the first pressure swing adsorption stage is 70-80% (V).
7. The method of a mobile pressure swing adsorption oxygen production plant according to claim 1 or 2, wherein the adsorption column of the first pressure swing adsorption section is packed with a 5A type molecular sieve or an X type lithium molecular sieve as a nitrogen balance selective adsorbent; the adsorption tower of the second pressure swing adsorption section is filled with carbon molecular sieve as a speed selective adsorbent.
8. The method of a mobile pressure swing adsorption oxygen production plant according to any one of claims 1 or 2, wherein a pressure swing adsorption drying section is added before the first pressure swing adsorption section for removing gaseous water from the raw material air to meet the requirement of the adsorption tower entering the first pressure swing adsorption section for moisture; the pressure swing adsorption drying section sequentially goes through at least two pressure swing adsorption process steps of adsorption A and purging P in a cycle period, and the gas in the purging P step is sourced from the vent gas of the adsorption A step outlet of the adsorption tower of the first pressure swing adsorption section and the desorption vent gas of the adsorption tower of the second pressure swing adsorption section.
9. The method of a mobile pressure swing adsorption oxygen production plant according to claim 8, wherein the drying section is filled with activated alumina as a desiccant: the adsorption tower of the first pressure swing adsorption section is internally filled with a 5A type molecular sieve or an X type lithium molecular sieve as a nitrogen balance selective adsorbent; the adsorption tower of the second pressure swing adsorption section is filled with carbon molecular sieve as a speed selective adsorbent.
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| Application Number | Priority Date | Filing Date | Title |
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| PCT/CN2020/084582 WO2021207903A1 (en) | 2020-04-14 | 2020-04-14 | Method for mobile pressure swing adsorption oxygen production device |
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| CN114053830A (en) * | 2021-12-17 | 2022-02-18 | 湖南卓誉科技有限公司 | Oxygen generation system and oxygen generation method |
| CN114471082B (en) * | 2021-12-27 | 2023-11-24 | 昆山欧拓气体设备有限公司 | Energy-saving VPSA oxygen production method and equipment |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1221642A (en) * | 1998-10-22 | 1999-07-07 | 中国人民解放军军事医学科学院卫生装备研究所 | Method for pressure variable absorbing preparation of high density oxygen from air |
| CN1583222A (en) * | 2004-06-11 | 2005-02-23 | 成都天立化工科技有限公司 | Method for producing oxygen by three-stage pressure swing adsorption apparatus |
| CN1597054A (en) * | 2004-06-11 | 2005-03-23 | 成都天立化工科技有限公司 | Improved two-stage pressure-varying adsorption method for preparing high-purity oxygen |
| CN102755811A (en) * | 2012-08-02 | 2012-10-31 | 南京圣火水泥新技术工程有限公司 | Moving bed pressure varying adsorption gas separation device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US5395427A (en) * | 1994-01-12 | 1995-03-07 | Air Products And Chemicals, Inc. | Two stage pressure swing adsorption process which utilizes an oxygen selective adsorbent to produce high purity oxygen from a feed air stream |
| CN103768891B (en) * | 2014-02-17 | 2015-11-18 | 上海穗杉实业有限公司 | A kind of two-stage series connection swing adsorption oxygen generating system and method for operating thereof that can improve oxygen recovery rate |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1221642A (en) * | 1998-10-22 | 1999-07-07 | 中国人民解放军军事医学科学院卫生装备研究所 | Method for pressure variable absorbing preparation of high density oxygen from air |
| CN1583222A (en) * | 2004-06-11 | 2005-02-23 | 成都天立化工科技有限公司 | Method for producing oxygen by three-stage pressure swing adsorption apparatus |
| CN1597054A (en) * | 2004-06-11 | 2005-03-23 | 成都天立化工科技有限公司 | Improved two-stage pressure-varying adsorption method for preparing high-purity oxygen |
| CN102755811A (en) * | 2012-08-02 | 2012-10-31 | 南京圣火水泥新技术工程有限公司 | Moving bed pressure varying adsorption gas separation device |
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| CN112041264A (en) | 2020-12-04 |
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